Hf-bf3 treating of secondary alkyltoluenes



Nov. 13, 1956 D. A. MCCAULAY ET AL 2,770,652

PIF- BF3 TREATING oF SECONDARY ALKYLTOLUENES l Filed oct. 3o, 1953 |NvENToRs= Dov/d A. McCall/ay BY 1r/bur E Lien,

United States Patent HF-BFs TREATIN G F SECONDARY ALKYLTOLUENES David A. McCaulay, Chicago, Ill., and Arthur P. Lien, Highland, Ind., assignors to Standard Oil Company, Chicago, Ill., a corporation of Indiana Application Gctober 30, 1953, Serial No. 389,380

6 Claims. (Cl. 2260-668) This invention relates to the rearrangement of certain secondary alkyltoluenes. More particularly the invention relates to the isomerization and/or disproportionation of isopropyltoluene and secondary butyltoluene. Still more particularly the invention relates to the production of essentially pure meta isopropyltoluene (rncymene) and 3,5-di-isopropyltoluene (3,5-di-isopropyl- 1-methylbenzene) The development of the hydroperoxide synthesis for phenol using isopropylbenzene as the starting material or substituted secondary alkylbenzenes has resulted in a demand for substituted Since certain phenols have particularly desirable properties for use as chemical intermediates, a demand has arisen for large quantities of various substituted secondary alkylbenzenes of high purity, i. e., about 95%, and also essentially pure, i. e., 99%, compounds. Of particular interest are meta isopropyltoluene` and 3,5-diisopropyltoluene. Meta isopropyltoluene is also of interest to the high polymer industry as a raw material for the manufacture of styrene type plastics having a softening point higher than that of polystyrene. The production of isopropyltoluene by the alkylation of toluene with propylene produces a mixture of the three isomers; therefore, industry is concerned With the prep-` secondary alkylbenzenes.`

from a feed containing at least one of the other isomers or mixtures of the meta isomer and substantial amounts of the other isomers. A further object is a process for the preparation of high purity meta secondary alkyltoluene without the simultaneous` production of significant 2,770,662 Patented Nov. 13, 1956 Ice amounts of poly-secondary alkyltoluenes.` A specific object is the preparation of essentially pure meta isopropyltoluene by the treatment of a mixture of isopropyltoluene isomers without simultaneously producing any appreciable amount of polyisopropyltoluenes. Other objects will become apparent in the course of the detailed description of the invention.

DISPROPORTIONATION In this process a secondary alkyltoluene` selected from the class consisting of isopropyltoluene and secondary butyltoluene is contacted under substantially anhydrous conditions and in the substantial absence of reactive hydrocarbons with at least an el'ective Aamount of BFa,

preferablyat 1 mol per mol of sec-alkyltoluene, and an amount of liquid HF at least sufficient to form a distinct acid phase, preferably about 5 to 2O mols per mol of sec-alkyltoluene; the contacting is carried out at a temperature between about 20 C. and about 80 C. for a time at least sufficient to permit an appreciable amount of rearrangement reaction; the HF and BFs are removed from the acid phase in order to recover polysecondary alkyltoluenes and a secondary alkyltoluene` fraction enriched in the meta isomer, with respect to the meta isomer content of the secondary alkyltoluene charged (unless essentially pure meta secondary alkyltoluene is charged).

ent, the feed must contain essentially only either `isop propyltoluene or secondary butyltoluene as the reactive component. p

in addition to the secondary alkyltoluene, the feed may contain non-reactive liquid hydrocarbons, It is to be understood that the term non-reactive liquid hydrocarbons is intended to mean thosehydrocarbons which are liquid at operating conditions and which are' inert to the action of the HF-BFs agent and do not participate in any reaction with the secondary alkyltoluene charged. Examples of reactive hydrocarbons are oleiins, xylene, di-ethylbenzene, ethyltoluene and ethyl,

benzene. Examples of non-reactive hydrocarbons are: isopentane, butane and hexane. Surprisingly enough, benzene is non-reactive and may be present in the feed. It is preferred that toluene be absent from the feed as its presence has an adverse eifect on the degree of disproportionation obtained.

The process utilizes ksubstantially anhydrous liquid hydrogen fluoride. not contain more than about 2 or 3% of water. Commercial grade anhydrous hydrolluoric acid is suitable for this process.

Under the conditions of the process, poly-alkylben- Zenes form a complex containing 1 mol of BFs, and, it is believed, 1 mol of HF per mol of poly-alkylbenzene. Therefore, at least enough liquid HF must be present to participate in the formation of the complex with the secondary alkyltoluene; in addition to this amount, sufficient liquid HF must be present to dissolve the complex which has been formed. In general, the presence of a distinct separate acid phase in the contacting zone indicates that at least the minimum requirement of liquid HF has been met. More than this minimum amount of liquid HF is desirable. Usually between about 3 and 50.m ols of liquidHF` are ,utilizedper molof. secondary alkyltoluene ychargetl.toithe process. Itis preferred to operate Vwith,` between about 5 vand, 20 .mols' of liquidl-IF pl'errnol` of ,secondary yalkyltoluene charged.

The process requiresthepresenceof atleast anPamount of .boren ,trilluoride,y sucient. to, .cause a rearrangement reaction to take place, specifically the. disproportionation of the secondary alkyltoluene to poly-alkyltoluene. While amounts y.ofiBEs as'small as-0.1. mol per mol of secondary alkyltoluenecharged will` cause an appreciablefarnount of'lrealfrangement.reactionto take place, it is' desirable tqoperate with about 0.5mo1 of B Fs.` Still moreuBFfhasa'benefieial elect on the degree ofthe rearrangement reaction andjas muchasS or more mols may .be used ,ipermolnof secondary alkyltoluene charged. When highpurity 3,5-di-secondary alkyltoluene is a desired product, Iat leastabout 1 mol of BFx should be used per` mol of', seconda'ry alkyltoluene charged, and it is preferred. to use betweenat least 1 and about2 mols of BFs per, mol of secondary alkyltoluene charged.

Whenth'e feed to.the pro,cess contains poly-alkylbenzones in addition to the secondary alkyltoluene, 1,mol of B Fa should be used per mol of said -poly-alkylbenzene in addition to ,thatset out above.

The, process may be operated with two liquid phases present 'irilthe contactinguzone. At high BFs usages, a gas-phase may also be present in the contacting zone, Thertwo liqui dphases= will be spoken of herein as the ranategphazseanddhe acidphase. The acid phase consists ofjliquidvHF', BH3', complex and dissolved hydrocar-bons. The rai'nate phase may be secondary alkyltoluenes4 in excessofi'that amount taken into the acid phase, or may be a mixture of 'secondary alkyltoluene andcinerthydrocarbons, ormayl be principally inert hydrocarbons. ,'InA the absence of substantial amounts of inert hydrocarbons., .theamount of raffinate phase is dependent upon the amount of BF3 utilized. When using about f1 molV of BF; per mol of secondary alkyltoluene e.^g., 0:9, vandin ,the substantial absence of inert hydrocarb'ons',ja1lv -or virtually all the secondary alkyltoluene willfgbeftaken into theacid phaseeither in the form of a complex or Yin solution. The presence of HF-BFspoly-alkylbenzene complexinr liquid HF very greatly increases Vthe solubility-of the liquid H'F for aromatic hydrocarbons and increasesgslightly the solubility of parafnic' hydrocarbons.' i

The presence of a rafiinate phase consisting principally ofiinerthydrocarbons,y such'as benzene and parains, has an-adverse'eiect-'on the degree and direction of conversion-ofthe -secondary alkyltoluene charged, even though'theoretically suflicient BF3 is present to complex.

all-o'the seconda-ry alkyltoluene charged. A substantial-,amount ofthe secondaryalkyltoluene-will remain in the raliinatetphase,y even Ywhen using somewhat more than `1 mol-fofJBFs perl mol of secondary alkyltoluene charged.-v The secondary alkyltoluene in the raflinate phase does -not undergo arearrangementreactio'n to any significant extent, even under conditions of good agita;-

The" liquid" hydrogen fluoride should 45,"- tion. The presence of dissolved inert hydrocarbons in the acid 'phase does not appear to have any adverse elf'ct on the degree or `direction of the rearrangement reactions.

In order to maximize the yield of conversion products, and to produce a di-secondary alkyltoluene product fraction consisting substantially of 3,5-di-secondary alkyltoluene, it is preferred to operate under conditions which form a single essentially homogeneous liquid phase in the contacting zone. A single essentially homogeneous liquid phase is attainable with a feed containing as much as 3 volume percent of parainic hydrocarbons. Large amounts of benzene and toluene may be dissolved in the acid phase, as much as 1 mol or more, per mol of complexed poly-alkylbenzene, depending on the amount of complex in the acid phase. (It is to be understood that a separate gaseous BF3 phase may also be present, but it is preferred that a minimum of free space be present in the contacting Zone and that sucient pressure be maintained to insure that essentially all the BFS is either in the complexed form or -isin physical solution in the acid phase.)

The degree andidirectiony of :the .disproportionation reaction are also determinedy by thetemperature of contacting and the `time ,of `contactinga denite relationship, existsbetween 1 the temperature,l time and .desireddisproportionation products. At.-y temperatures4 below,- about --25 C. no appreciable disproportionation takes place even lat'contactingtimesof---severaldays.A At temperatures of C. onhigherysidereactions such as alkyl group cracking occur and the direction of the disproportionation changes; this is evidenced by the production of a` wide boilingrange.v product. mixture. The practical upper.. limit fortheoperation of the disproportionationprocess is..about.-{80 C. Appreciableamountsof disproportictnation` product are ,obtained in a notexcessively. longtime at atemperature of about -20 C. The preferred range of operatin'g temperatures for the disproportionationl process isbetween about +10 C.v and about +60 `C."

Thecontactingtime has an important effect on the course or" the Arearrangement reactions. At least sufficient timemust be provided at .the vparticular temperature of operationin ,order tol obtain.an appreciable' amount of disproportionation products. As thecontacting time is'. increased, ata constanttemperature, the amount of'disproportio'nation product increases. The disproportion-v ation reaction appears to produce the di-secondary alkyltoluene .as thetrst produ-ch. Dependent upon the tem-= perature, .a n'ite period of time elapses between the appe'arance ofdt :`te'ctable` amounts of the di-'secondary alkyl-v tolueneproduct and the appearance of the tri-secondary alkylto'hine. product operation, Vthe longen the time'lapse betweenthe appearance of 'thedi-'tderivative andY the appearance of the triderivative.`

With increasing lcontacting, time, at. constant` temperature, theamount of poly-secondary alkyltoluenel product graduall'yincreases at the expense :of secondary alkyl` toluene charged.l Gradually the amount Vof. the.. triderivative' increases and eventually the tri-derivativeI continues to-increase withsimultaneous `disappearance of the di-dcrivative, At higherv temperatures and prolonged secondary alkyltoluene will'be found lin the reaction v* Thusby adjusting the .temperature and produtmxture time of contactingLit'is possibleto control the relative amounts. of di-Y and tri-derivatives produced in the dis-.

proportionation process.

The disproportionation reaction can` be controlled.,

within .experimental error, to produce. di-,secondajry alkyl-I toluenefastessentially .th only poly-secondary alkylthiene product. When the' di-s'econdary alkyltoluene is' the The lowerthe temperature of only desired poly-secondary alkyltoluene disproportionation product, the contacting temperature should not exceed about -|30 C. The lower temperature of operation is about C.

The contacting time at C. must be short enough to essentially eliminate the disproportionation to the triderivative. At about -l30 C. the permissible maximum time of contacting is about 5 minutes to essentially avoid the formation of the tri-derivative. The lower the temperature of contacting, the longer the contacting time permissible while avoiding the formation of detectable amounts of the tri-derivative. At about y-1-107 C. contacting temperature, the permissible maximum 'time is about 60 minutes; at about 20 C., the permissible maximum contacting time is several days. Thus in order to avoid the formation of appreciable amounts of trisecondary alkyltoluene, the disproportionation process must be carried out, at a temperature of about +30 C., for a maximum contacting time of about 5 minutes. The lower the temperature of contacting, the longer will be the corresponding permissible maximum contacting time.

Even when using smaller amounts of BFz, the predominent di-secondary alkyltoluene product is the 3,5- di-secondary alkyltoluene, i. e., the symmetrical contiguration. The use of slightly less than l mol of BF3 per mol of secondary alkyltoluene charged gives a disecondary alkyltoluene product fraction consisting substantially of 3,5-di-secondary alkyltoluene which is described as high purity 3,5-di-secondary alkyltoluene (3,5- disecondary alkyll -methylbenzene). The use of at least l mol of BFS and preferably somewhat more, e. g., 1.3 mols, gives essentially pure 3,5-di-secondary alkyltoluene as the secondary alkyltoluene product. By careful control of the contacting time it is possible to produce a di-secondary alkyltoluene product fraction which is, within the error of the analytical procedure, pure 3,5-di-secondary alkyltoluene.

When the charge to the disproportionation process consists of the ortho isomer, the para isomer, mixtures thereof, and mixtures of the meta isomer and at least one other isomer, which other isomer is present in substantial amounts, the acid phase contains a reaction product mixture wherein the secondary alkyltoluene fraction is enriched with respect to the meta isomer when compared with the charge. When operating under essentially single liquid phase conditions and with at least l m01 of BFS per mol of secondary alkyltoluene charged, the reaction product mixture contains essentially pure meta secondary alkyltoluene as the secondary alkyltoluene component, i. e., the ortho and/ or para isomers are isomerized to the meta isomer.

When the charge to the disproportionation process de scribed above is a secondary alkyltoluene selected from the class consisting of isopropyltoluene and secondary butyltoluene, the reaction product mixture contains relatively large amounts of thedi-secondary alkyl derivative even though high temperatures and long contacting times are used. The use of secondary alkyltoluene as the charge results, at long contacting times, in a mixture wherein the di-secondary alkyltoluene is a major component of the reaction product mixture.

When it is desired to maximize the yield of the tri secondary alkyltoluene product fraction, the charge to the disproportionation process should be the corresponding cli-secondary alkyltoluene. The use of an isomer or a mixture of isomers of di-secondary alkyltoluene which are selected from the class consisting of di-isopropyltoluene and cli-secondary butyltoluene as the charge to a disproportionation process, wherein sufficient liquid HF and BFs are used to form a single essentially homogeneous phase, at a temperature between about +30 and +60 C. for a suitably long contacting time, results in a reaction product mixture wherein the di-secondary alkyltoluene forms only a minor part of the reaction product mixture.

The invention is limited to the HF-BF3 treatment of isopropyltoluene isomers and secondary butyltoluene isomers because successful treatment of the secondary pentyltoluenes requires very different operating conditions. Even at temperatures on the order of +20 C. and contacting times as short as l5 minutes, the secondary pentyltoluenes undergo rearrangement of the pentyl group and also cracking of the pentyl group. In addition, cyclization reactions occur and substantial quantities of indanes and tetralins are formed. Rearrangement of the pentyl group is particularly prominent when 3-to1ylpentane is the charge to the HF-BFa contacting zone. The 3-tolylpentane isomerizes to give good yields of the Z-tolylpentane derivative, particularly the l methyl-2,4 bis(2pentyl) benzene disproportionation product. Rearrangement of the pentyl group is not present to any large extent when 2-toly1pentane is the charge to the HF- BFs contacting zone. It is to be understood that by suitable adjustment of the temperature and time of contacting it is possible to minimize side reactions.

ISOMERlZATlON The isomerization reaction considered herein is the shift of position of substituent alkyl groups on the benzene ring without rearrangement of the alkyl group itself. The isomerization process comprises contacting under substantially anhydrous conditions and in the substantial absence of reactive hydrocarbons a secondary alkyltoluene selected from the class consisting of the ortho isomer, the para isomer, and mixtures thereof with at least an effective amount of BFa and an amount of liquid HF at least sufficient to form a distinct acid phase; the contacting is carried out at a temperature of not more than about -30 C., for not more than about 30 minutes; as the temperature of contacting is lowered, the permissible maximum time of contacting may be increased; and removing HF and BFS from the acid phase under conditions to substantially avoid rearrangement reactions and recovering from the reaction product mixture a secondary alkyltoluene fraction containing the meta isomer. A feed, containing mix-tures of the meta isomer and a substantial amount of at least one of the other isomers, when treated with at least about 'l mol of BFs per mol of secondary alkyltoluene charged, and other conditions as given above, produces a reaction mixture enriched with respect to the meta isomer relative to the charge to the process.

By carrying out the isomerization process in the presence of added toluene, the process may be carried out at temperatures as high as about +20" C. without pro# ducing appreciable amounts of disproportionation reaction products, It is preferred to use at least about l mol of added toluene per mol of secondary alkyltoluene charged.

The charge to the low temperature isomerization process contains a secondary alkyltoluene selected from the class consisting of the ortho isomer, the para isomer, mixtures thereof, and natural mixtures of all three isomers. When using at least about l mol of BFa per mol of secondary alkyltoluene charged, the feed may contain mixtures of the meta isomer and a substantial amount of atleast l other isomer.

The feed to the isomerization process may be of the same type as the feed to the disproportionation process. However, for reasons pointed out hereinafter, the presence of toluene in the feed to the isomerization process is beneficial.

The isomerization process, like the disproportionation process, utilizes substantially anhydrous liquid hydrogen fluoride. The isomerization process and the disproportionation process utilize liquid HF to the same degree.

The isomerization process requires the presence of at least an amount of BFs sucient to cause an appreciable 2,17.rf.crece;y

amount ',ofxisomerization :of the ,ortho and. para` isomers to the meta isomer. While amounts of BF3 as small,. as '=0.`1:'m,o,l fp,er, 1mol of secondaryalkyltoluenencharged causefanappreciable amount of isomerizationwtofvtake place, ituis ,desirable Ito. operate. with motel-than this amount, e. g. about 10.5 mol` of BFa. As much as `5 or` moremols of BFS may be used perfrnol .ofl'seoondary alkyltoluene.lV charged. has,I anextremely beneficial elfeet on the `degree ,rofisomerization obtained. When slightly less than l mol iof Bix spermol of; secondary alkyltoluene charged is used, engr, r0.9-mol, the reaction product mixturecontai-ns high purityrneta-fsecondary alkyltoluene as the secondary alkyltoluene fraction. Inorder to obtain;I the A'conversion of-theseoondary alkyltoluene charged. toessentially pure` metasecondaryalkyltoluene, the process is operated with between at least -l and about 2 mols of -BFa per mol of secondary alkyltoluene charged.

'llheisomerization process may be carriedout with two liquid phases in the contacting zone as has been described above in the disproportionation process. However, in order to maximize the yield of the isomerization product, and to improve the purity of the desired meta secondary alkyltoluene, it is preferred to operate under conditions whichform a single essentially homogeneous liquid phase in :the contacting zone.

The isomerization reaction considered hereinis the shift of.- position of substituent alkyl groups on thebenzene ring Aw-ithout rearrangement of theV alkyl group itself. This isomerization reaction proceeds at a much faster rate, at lower temperatures, than does the reactionwherein alkyl groups are transferred from one benzene ring to another benzene ring, i. e., disproportionation. It is possible by suitably adjusting the temperature and time of` contacting to essentially avoid the formation of disproportionation products and limit the course ,of the rear-Y rangement reaction to isomerization alone. (It is to be understood that the term to essentially avoid is intended to mean within the error of the analytical procednres now available to the art, for example, ultra-violet and infrared techniques.)

At temperatures of not more than about C. it is possible, by limiting the contacting time to not more than about minutes, to isomerize substantially all the ortho and/ or para isomers present in the charge` tothe corresponding meta isomer, when at least about l mol of BF3 is used per mol of secondary alkyltoluene charged. As `thetemperature of contacting is lowered, the permissible time of contacting may be lengthened without formation of appreciable amounts of the undesired disproportionation reaction products. When the process is operated .at about 20 C. for a time of not more than about 5 minutes, the reaction product mixture contains essentially no disproportionation reaction products; at a BF3 usage of at least l mol of BFs per mol of secondary alkyltoluene charged, and these conditions of time and temperature, essentially pure meta secondary alkyltoluene is obtained as the reaction product. At contacting zone temperature of about 30 C. the maximum permissibley contacting time is about l0 minutes.

Obviously operation at these low temperatures and very short contacting times has a serious effect on the commercial practicality of this isomerization process. It has been found that the presence of toluene in the feed to the process has a remarkable eifect on the rate at which disproportionation proceeds. The presence of substantial amounts of toluene in the charge slows down the disproportionation reaction rate to such an extent that it is possible to essentially eliminate the products of disproportionation at temperatures where substantial quantities 0f the di-secondary alkyltoluene would have been formed, in the absence of added toluene.

The isomerization process can be carried out withoutk formation of appreciable amounts of vdisproportionation products'at temperatures of' not more than Aabout +20 Increasing the` .amount of BFS;

C. .Whenfstl'letzhargel tofjthe process comprises. essentially;

allnollntg-cf` disproportionation products formed'is deg;-

pendent upon temperature, time and amount of toluene addedg,ityis;preferredztouse vat least about; 1 mol 'offvadcled toluene andr preferably-the maximum amount :soluble invthe.acidiphase :shouldgbe used. When operatingfwith; about -1 mol of, to1ueneinthe feed per mol-.- of secondary alkyltoluene,` ypresent-..therein, the isomerization process` may rbcY carried, out at about +209 C. foran about 5v minute maximum contactingv time; atA about 0 C. `for an about 30 minute maximum contacting time,` andat about-` -20- C. for anabout `2 ,hour maximum `contactingtime.A Under this relationship of. ytemperature A and` time, andi at least ,1 molffof BFS yper-mol ofl secondary `alkyltoluene charged, an essentially purelmeta secondary alkyltoluene product is obtained, .without `forming any appreciable amounty of the. corresponding `di-secondary alkyltoluene,

and -{30` C. andl a suitably .short time, it is possible to obtainessentially pure A3,5-di-secondary alkyltoluene asthe,

reaction product, toy the essential exclusion of disproportionation `toni-secondary alkyltoluene.

PRODUCT RECOVERY The reaction-product mixture may be recovered from the acid phase `byvarious methods'. Probably the simplestprocedure and one mostsuitable for laboratory workl consists ofy adding the acid'vphase to crushed ice or the acidfphaseimay be contacted with coldl aqueous alkaline solution, such as sodiumhydroxide, potassium hydroxide andl ammonia. It is desirable to prevent rearrangement reactionsby the -use of a cold aqueous reagent.

The hydrocarbonsoriginally present in the acid phase appear as an upper oillayer above a lower aqueous layer. The upper oil layer may be separated by decantation and may be treated with dilute aqueous alkaline solution to removetany remaining HF and BFz occluded therein.

Both HF and BFg are relatively expensive chemicals andv it is desirableinan economic process to recover these and: to recycle them for reuse in the process. The HF and the BFs may be readily `removed from the acid phase by heating the acid phase or by applying a vacuum thereto. The HF and the BF3 distill overhead and may be recovered for reuse in the process. Zenes and/or tri-alkylbenzenes are the principal complex forming hydrocarbons, the complex may be decomposed at relatively .low temperatures by the use of vacuum distillation. The :tetra alkylbenzene and higher alkylbenzene complexesarestable and must be heated to relatively high temperatures, for example, C. or more in order todecompose the complex.

The rearrangementreaction proceeds from the time that the complex is formed until the complex is decomposed, assuming that a suitable temperature exists. When it is desired torproduce essentially only one rearrangement reaction product, for example, meta isopropyltoluene from para isopropyltoluene, or 3,5-di-isopropyltoluene from isopropyltoluene, it is necessary to take into account the total time elapsing from the time that the complex of isopropyltoluene and HF-BFa has been formed till the time that it has been decomposed in the distillative decomposition procedure. Thus, when using distillative decomposition procedure, it is necessary to consider the residence time of the complex in the decomposing Zone as a part of the contacting time. Also,it is necessary to consider the temperature maintained in the decomposing zone when av lparticular product or a particular ratio off products is de.`

When di-alkylbenl arr/'desa sir'ed. Generally the temperature in the decomposing zone should be no higher than that in the contacting zone, when operating to proluce meta secondary alkyltoluene. The distillative decomposing zone may be perated at temperatures as low as about -20 C. by the use of high vacuum therein.

IThe `di-secondary alkyltoluene at moderate temperatures disproportionates very slowly to the tri-secondary p alkyltoluene. Therefore it is possible to distillatively decompose the complex of di-secondary alkyltoluene at temperatures as high as 4G or 50 C. if the acid phase is very rapidly raised to that temperature from the reaction temperature of below about |30 C. and the HF and BFz are very quickly removed from the heated acid phase.

fThus the recovery of the meta secondary alkyltoluene product Without back isomerization to ortho and para isomers or disproportionation to the di-secondary alkyltoluene is the most difficult recovery to lbe :made by distillative decomposition of the complex. It is obvious that operation at very low temperatures such as 0 C. or lower involves an expensive high vacuum operation since liquid H'F boils at +20 C. .at atmospheric pressure.

yThe preferred method of recovering high purity meta secondary alkyltoluene from an acid phase Without back isomerization or disproportionation is the displacement of the meta secondary .alkyltoluene `from its HF and BiFa complex =by an alkylbenzene 'which forms a more stable HF and BFa complex. Broad'ly, the displacer is a poly- Ialkylbenzene containing at least three .alkyl groups `which alkyl groups are selected `from the class consisting of 'normal and secondary Iand which contain not more than 4 carbon atoms. Normal alkyl groups are methyl, ethyl, n-propyl and n-butyl. The secondary alkyl groups are isopropyl and secondary butyl.

Pentamethylbenzene and hexamethylbenzene are particularly effective displacers. However, the complexes formed `by these compounds :are so stable that quite elevated temperatures are necessary to decompose the comp'lexes in order to recover the HF and BFS. Therefore, Where economy is desirable, these compounds should not |be used .as displacers.

"The preferred tri-alkylbenzenes have the symmetrical conguration, i. e., 1,3,5tri-alkylbenzene. The preferred tetra-alkylbenzenes possess the l,2,3,5 conguration. '.T'hese displacers are preferred because they `donot tend to undergo rearrangement reactions and have better displacement effectiveness than the other isomers. The preferred displacers are mesitylene, tri-isopropylbenzene, diisopropyltoluene and isodurene.

As it is normally impractical to operate under conditions wherein absolutely no dii-secondary alkyltoluene is produced, it is desirable to operate with a displacer Which Will not complicate the problem of recovering the byproduct, di-secondary alkyltoluene. Therefore it is preferred to use las the displacer `in the process of this invention a poly-secondary alkyltoluene, for example, diisopropyltoluene, or di-secondary butyltoluene, corresponding to the sec-alkyl group charged.

Theoretically, 1 mol of added displacer will replace 1 mol of secondary alkyltoluene. However, greater .amounts of displacer should be used. The amount of -displacer used is dependent upon the total recovery of secondary alkyltoluene desired and also the effectiveness of the contacting of the acid phase and the displacer. lt is preferred to operate with lbetween about 2 and 4 mols of displacer per mol of secondary alkyltoluene present in the acid phase.

`It has been pointed out before that the acid phase possesses an extremely high solubility for aromatic hydrocarbons. Quite a large amount of displacer can be added to the acid phase Without apparently displacing any secondary alkyltoluene; the displaced secondary alkyltoluene a remains dissolved in the acid phase. By the use of very `l() large amounts of displacer, it is possible to produce .a second liquid phase which comprises displaced secondary alkyltoluene and displacer.

Since parainic hydrocarbons are soluble in the acid phase to only a relatively small extent, it is possible to wash from the acid phase-displacer solution the displaced secondary -alkyltoluene The wash hydrocarbon must be inert to the action of HF and B133 and non-reactive with the alkylbenzenes present in the acid phase. Benzene and toluene may be used as wash hydrocarbons. It is preferred to use as the inert hydrocarbon a low Iboiling liquid parain `such as propane, butane, pentane and hex-ane.

The wash hydrocarbon may be introduced into 'the acid phase-displacer solution simultaneously `with the displacer, preferably as -a single solution; or the wash hydrocarbon may be introduced into the acid phase after the addition of the displacer. In order to avoid rearrangement reactions, -it is preferred to introduce the wash hydrocarbon substantially simultaneously after the introduction of the displacer.

lIt is preferred to carry out the displacement operation in a continuous countercurrent tower; in such an operation the acid phase is introduced in .an upper portion of the tower, the d-isplacer is introduced at a lower portion of the tower and the inert wash hydrocarbon is introduced at a point of the tower lbelow the point of entry of the displacer.

-The `amount of inert wash hydrocarbon introduced must be enough to remove substantially all the displaced secondary alkyltoluene. In general, the amount of inert wash hydrocarbon used is between about 50 and 500 volume percent based on secondary alkyltoluene displaced, pre-ferably between about vand 250 volume percent.

In order to avoid rearrangement reactions, the displacing zone should be operated at a temperature and for a contacting time such that essentially no rearrangement reactions `take place therein. Thus, the contacting time `in the displacing zone and the temperature therein must be considered in determining the total contacting time to be utilized in the process.

EXAMPLES The results obtainable by the invention are illustrated by several examples set out below. The tests were carried out using a carbon steel reactor provided with a 1725 R. iP. M. stirrer. The order of addition of materials to the reactor was: `(il) para cymene or para cymene and toluene of CP quality (2) commercial grade anhydrous liquid HF and (3) .commercial grade B133. The contents of the reactor were agitated during the addition of the HF-BF3; the agitation was continued while the reactor was brought to the ldesired contacting temperature and maintained during the contacting time. All the tests were carried out under conditions such that only one liquid phase was present in the reactor. The contents of the reactor were withdrawn into a polyethylene vessel (filled with crushed ice. An upper aqueous hydrocarbon layer formed above a lower aqueous layer. The hydrocarbon layer was decanted and washed with dilute ammonia hydroxide solutio-n to remove HF and BFs. The neutral hydrocarbons were water washed to remove traces of ammonium hydroxide.

The hydrocarbons recovered from the reactor lwere fractionated in a laboratory distillation column provided iwith about 30 theoretical plates. Each product frac- Ition was analyzed by a combination of boiling point, specific gravity, refractive index, and ultra-violet and infrared technique.

Tests were also carried out wherein the hydrocarbons were recovered from the acid phase by distillative decomposition thereof and by the displacement procedure using mesitylene as the displacer.

Theitresultsithese tests are .set ,out ;in Tabley .I.

In` this.. :test the displacing,solutionconsistedof L35 TABLE. I

Test, Not.-. 1 2 3 4- 5b s Charges..

pCymene, mols 1. 60 2. 25 1. 27 0. 64 1. 3 1.0 Tolueneffmolse; none nonev 1. 46 0. `70 l. 5 1. l Toluene/Cymene mol ratio 1.15 1.09 1.15 1.1 HF/Cymene mol rat1o- 15. 6 15. 5 27. 5 27.4 26. 9 27. 1 BFz/Gymeue m01ra1310 1. 50 1. 19 2. 32 2. 19 2. 19 v 2. 30 Temp rature,- C.- -20 +13 +13 +13 +12 +62 Time, inuteS 30 30. 3() 30 30 30 Reaction Product Mixture, m01 percent: f

Ran.- i Acid ate. f Phase Toluene 4. 4 34 55 46` 73 61. 4 61 o-isopropyltoluene O 0 O 0 0. 6 0 89. 5 27.-' 38 r 53- 6 21.6 22.5 Trac ca. 0.1 ca. 0.2 1 ca. 1 5.6 ea.0.2 G. 1 39' 7 0 20 10. 8 12. 6 0 0 0 0 f 0 0 8. 7

Cymene disproportionated, percent l 72;' 18 13 40: 52

Displacement .procedure 95%ot-isopropyltoluene.taken intomanate phasedseetexty., b Distllatve.decomposition procedure using135 minute total time at +22D C. (see text).

Test l Inl lthis f test thecontacting was continued :for i -3 0 minutesv at.=--2()" I C. The' reactionl product mixture contained about 6 mol percent of 3,S-di-isopropyltoluenerl Withinv experimentalerror no other isomer-of di-isopropyltoluene was-present.` The isopropyltolueneproduct fractionconsisted almost entirely of the meta isomera` Only ltrace amounts of-'the'vparafisomer were-found.y Even-at this lowtemperature,` the para isopropyltoluenecharged isomcrized essentially completely to the vmeta v coniigura` tion.

Atethis fairly long contactingy time Yof `30 minutes, :about 10%" of-the `isopropyltoluene charged had dispropor tionated to di-isopropyltoluene.

Test 2 Thisrun. was carried out` under'conditionsvery much; like those of Test 1 except thatthecontacting..temperafv ture contained only 27% of isopropyltoluene. Tests'd v and'vZvshowy that in 'the absence of addedftoluene,itis y necessary vto operate at low temperatures, -in/.ordento obv tain isomerization ofthe--para/isomento the nietaI isomer without simultaneously obtaining substantial amounts of disproportionationreaction products.

T est 3 In this test'about equalmolar amounts-ofpara cymenevr and toluene were charged. Averyilargefexcess of BFa was lalso used: The contacting temperature and timewere the same as those-used in-Test-2,i. e., +l3" C.' and -30 minutes.

The reactionproduct mixture contained only 7% of 3 ,i5-di-isopropyltoluene and -about 8%ofiessentially pure meta isopropyltoluene.v tolucnef'per' molhof para 4cymene. chargedflimited/fthe The presence of :aboutil mol-o disproportionation .in thisl test, tci-l8'%'v ofthe. -cy1nene= charged.

This is a dramatic'contrastwwith.fthe-1.72%4

disproportionation obtained in .Test 2,1`whieh.isessentially,

identical with Test .exceptsforfthe presence@f added.;

toluene in Test 3.

Test 4 Test 4 was carried out at essentially the same operating conditions as Test 3. mixture was recovered by the displacement procedure.

However, thereaction product *cymene isomers.

molsofmesitylene and v29,() m1. 4of n-pentane. This solution was .cooled tothe .reaction temperature ofl +139, C..y and was, added to the reactorimmediately aftery .the,30, minute contactinggtime.. The total contents ofthe, reacr. tor .were agitated for `10 minutes, vatabout .+137l C.;. then` lthe contents of the reactor were ,allowedlo settle.

for `10 minutes. At ythegend of the settling time each layer present inthe reactor, i. e., rainatephaseand acid phase .v were `withdrawn separately into polyethylene,vesselszfilled The `hydrocarbons were recovered with crushed ice.

separately` fromleach phase. In this test 2.4 mols of mesitylene were used per mol,- of isopropyltoluene present Y in..thereacti0n product mixture. The n-pentane usage was, 34.0A volume percent based` on the isopropyltoluener.,

present `in the reactor.

The rainatejphase consisted A of toluene, nieta isopropyltoluene, a very slight amountof para isopropyl-V toluene,r 12%.1of the mesitylene ichargeduand essentially;

all of the n-pentane charged.

The hydrocarbons recovered from the acid phase consisted` Zol a slightl amountofA n-pentane, 88%v of' the mesitylenercharged and isopropyltoluene fraction consist-k ingqofthemeta ,isomer and an.appreciablesamount offv di jisopro,py1to1uene. The 1disproportionation taking place in thisrun was about 13% of the v,cyrnene charged, 'which amount is inexcellent yagreement with 'the resultsobt'ained `in Test 3.'

This test shows that little or no further reaction occurs with'respect to the ,displaced isopropyltoluene after the. displacingsolution has been added to the acid. phase, v

even thouglrthe displacingsolution and the acid' phase addition.

Test f5 This test was carried yout under conditions, essentially identical with those of Test 3.` However, ,thereaction product mixture ofhydrocarbonswas recovered from the single' homogeneous, phase ,byydistillative decomposition thereof.

Atfthe completion ofthe 30 minute ,contacting time,

'the temperature. of the reactor wasu raised to +22',j' C.,-room temperature-anda vacuum -applied to the reaction zone.. The vapors were withdrawn from .the

reactor as rapidly as the overhead line would permit." Owing to thesmall size of theoverhead line, the distil 'lative decomposition took l135-minu 'tesl to -remove alllth'e HF and BFs from thereactor.

In this test;4 0%`fof the cymene charged'was4 di-spropor-f areintenselyagitated for some Vminutes after the initial emmene `contained measurable amounts of the ortho isomer as well as a large amount ofthe paraisomer; the meta l isomer was the predominant component.

isopropyltoluene had taken place.

This test shows that it is necessary 'to carry out the` distillative composition at low temperature and at a very rapid lraten of HF and BFs removal in order to avoid undesired isomerization and disproportionation reactions.

Test

This test was carried out to observe the effect of elevated temperature on the disproportionation of isopropyltoluene in the presence of added toluene. This test was carried out for 30 minutes at a contacting temperature of |52 C. The reaction product mixture contained about 13% of 3,5-di-isopropyltoluene and about 4% of tri-isopropyltoluene. The total disproportionation was 52% of the isopropyltoluene charged.

This test shows very graphically the adverse eiect on the degree of disproportionation of the presence of added toluene. In Test 2, which was carried out at a 40 lower temperature, in the absence of added toluene, 72% of the isopropyltoluene charged was disproportionated.

In spite of the relatively low amount of disproportionation, approximately 20% of the disproportionation product consisted of the tri-isopropyltoluene. This test indicates that lat elevated temperatures the disproportionation reactions tend to form tri-isopropyltoluene at the expense of the di-isopropyltoluene. The isopropyltoluene present in the reaction product mixture is about the same in Tests 2 and 6.

ILLUSTRATIVE EMBODIMENT The annexed figure, which forms a part of this specification, lshows an illustrative embodiment of a method of carrying out the invention to produce essentially pure 3,5-di-isopropyltoluene by disproportionating cymene. The figure is schematic land many items of equipment have been omitted, such as pumps, valves, etc., as these may be readily :added thereto.

One thousand gallons a day of feed from source 11 are passed by way of lines 12 and 13 into heat exchanger 14. From exchanger 14 the feed and recycled isopropyltoluene, 200 gals./ day, are passed by way of line 16 into line 17. In this embodiment, the feed consists of a mixture of all the isomers of isopropyltoluene which have been obtained by the alkylation of toluene with propylene, in the presence of Ialuminum chloride catalyst; the mixture contains about 50% of the meta-isomer. (In an integrated operation, the total reaction product consisting of toluene, isopropyltoluene isomers and di-isopropyltoluene isomers may be charged to the HF-BF3 isomerization process, thereby avoiding 'a fractionation operation.)

Anhydrous liquid hydrogen uoride, 2300 gals/day (14 mols/mol of isopropyltoluene) is passed from line 26, through heat exchanger 27 and line 28 into line 17. Heat exchangers 14 and 27 lower the temperature of the isopropyltoluene land the liquid HF to a temperature of labout C. This temperature is about 5 C. lower than the desired reaction temperature of -l- C.

The contents of line 17 are introduced into mixer 31 which is provided with heat exchanger means 32. 5500 lbs. per day of BFa (1.2 mols/mol of isopropyltoluene) from line 29 are introduced into mixer 31. Mixer 31 is an apparatus able to rapidly ntermingle the isopropyltoluene, liquid HF and BFa. Ihe reaction of the isopropyltoluene, HF and BFS to form the HF-BFa-isopropyltoluene complex is highly exothermic. The heat exchanger means 32 withdraws heat and prevents the temperature at the discharge end of mixer 31 rising above +15 C.

An acid phase consisting ol liguidtHFydissglved complex, toluene and BF@ isdiscliarged-from mixer V31. About 1100` p. s. i. g. of `pressure are wmaintainedonthe system to keep -the excess `BFS 4in theacid phase. The single homogeneous acid phase is passed from -rnixerlby w'a-y oflineltinto-reactor34. l 't t Y -Ieactor :34 Ais lprovided t with .heat exchanger t means `36 and 37. Agitation is not needed to assist-the reactioncrate :because of the single .phase` system `existing `in the reactor. To insure the maintenance `of va substantially .uniform temperature of -l-15 C. throughout the reactor, reactor 34 is provided with bales 38a, 3811 and 38C and motor driven agitator means 39.

The `acid phase is withdrawn from the top of reactor 34 and is passed by way of line 41 into decomposing zone 43. The rearrangement reaction starts as soon as the isopropyltoluene complex is formed and continues until the complex is decomposed by distilling o the HF and BFa. Therefore the contacting time is measured as the time in mixer 31, reactor 34 and part of the total time in decomposing zone 43. In this embodiment, a total time of 'about 50 minutes is utilized. Under these conditions only a very slight amount of tri-isopropyltoluene is formed. (Other methods for complex formation, for temperature control and for obtaining the proper amount of contacting may be readily devised.)

Decomposing zone 43 is provided with internal heater 44 and some fractionation means, not shown. The ternperature of +40 C. in zone 43 is Ihigh enough to readily decompose the HF-BFs .complexes but not high enough to cause appreciable further disproportionatilon.

HF vapor and BFS gas are withdrawn from zone 43 and passed by way of line 47 into heat exchanger 48. In heat exchanger 48, the HF vapors are condensed and a liquid-gas stream is passed by way of line 49 into gas separator 51. BFa is withdrawn from gas separator 51 and is recycled by way of lines 53 and 29 to mixer 31. Make-up BF3 is introduced from source 56 by Way of valved line 57 into line 53. Liquid HF is recycled by way of lines 61 and 26. Make-up HF is introduced from source 62 by way of valved line 63 into line 61.

The bottoms fraction from decomposing zone 43` consists of isopropyltoluene, di-isopropyltoluene and toluene. The bottoms fraction is withdrawn and introduced by way of line 71 into fractionation zone 72, shown schematically herein. A toluene fraction, 345 gals/day, is withdrawn to storage by Way of line 74. A product fraction consisting of essentially pure 3,5-isopropyltoluene 660 gals./ day is passed to storage by way of line 76. A bottoms fraction of tri-isopropyltoluene, 4 gals./ day, :is Withdrawn by way of line 78.

As the conditions in decomposing zone 43 cause some back-isomerization of the meta-isopropyltoluene to the ortho and para isomers, the mixed isopropyltoluene fraction, 200 gals./ day from fractionation zone 72 is recycled by way of lines 79 and 13, etc. to mixer 31.

What is `claimed is:

1. A process which comprises contacting, under substantially anhydrous conditions, a charge consisting essentially of at least one isomer of a single secondary alkyltoluene selected from the class consisting of isopropyltoluene and secondary butyltoluene with at least one mol of BFa per mol of secondary alkyltoluene char-ged and at least sufficient liquid HF to panticipate in complex-formation and to dissolve said char-ge to form a single essentially homogeneous liquid phase, at a temperature between about 20 C. and about +30 C. for a permissible maximum time of about 5 minutes at +30 C. and several days at 20 C., the lower the temperature of contacting, the longer the correspondin-g permissible maximum time, said conditions of time and temperature resulting in the format-ion of 3,5-di-sccondary alkyltoluene as essentially the only alkyltoluene reaction product, removing the HF and BFz;A from the `reaction mixture under conditions to substantially avoid rearrangement reactions and recovering from said reaction product mixture essentially 5. The process of claim 1 wherein said alkyltoluene is pure 3,5-di-secondary alkyltoluene. a mixture of secondary butyltoluene isomers.

2. The process of claim 1 wherein said temperature is 6. The process of claim 1 wherein said alkyltoluene is about +10 C. and said permissible maximum time is para-isopropyltoluene. about 60 minutes. 5

3. The process of claim 1 wherein said HF usage is be- References Cited in the me 0f this Patent tween about 3 and 50 mols per mol of secondary alkyl- UNITED STATES PATENTS toluene Charged 2 l521 444 Brooke et al Se y i pt. 5, 1950 4. The process of claim 1 wherein said alkyltoluene is a 2,644,017 McCauley June 30, 1953 mixture of isopropyltoluene isomers. 10 

1. A PROCESS WHICH COMPRISES CONTACTING, UNDER SUBSTANTIALLY ANHYDROUS CONDITIONS, A CHARGE CONSISTING ESSENTIALLY OF AT LEAST ONE ISOMER OF A SINGLE SECONDARY ALKYLTOLUENE SELECTED FROM THE CLASS CONSISTING OF ISOPROPYLTOLUENE AND SECONDARY BUTYLTOLUENE WIUTH AT LEAST ONE MOL OF BF3 PER MOL OF SECONDARY ALKYLTOLUENE CHARGED AND AT LEAST SUFFICIENT LIQUID HF TO PARTICIPATE IN COMPLEX-FORMATION AND TO DISSOLVE SAID CHARGE TO FORM A SINGLE ESSENTIALLY HOMOGENEOUS LIQUID PHASE, AT A TEMPERATURE BETWEEN ABOUT -20* C. AND ABOUT +30* C. FOR A PERMISSIBLE MAXIMUM TIME OF ABOUT 5 MINUTES AT +30* C. AND SEVERAL DAYS AT -20* C., THE LOWER THE TEMPERATURE OF CONTACTING, THE LONGER THE CORRESPONDING PERMISSIBLE MAXIMUM TIME, SAID CONDITIONS OF TIME AND TEMPERATURE RESULTING IN THE FORMATION OF 3,5-DI-SECONDARY ALKYLTOLUENE AS ESSENTIALLY THE ONLY ALKYLTOLUENE REACTION PRODUCT, REMOVING THE HF AND BF3 FROM THE REACTION MIXTURE UNDER CONDITINS TO SUBSTANTIALLY AVOID REARRANGEMENT REACTIONS AND RECOVERING FROM SAID REACTION PRODUCT MIXTURE ESSENTIALLY PURE 3,5-DI-SECONDARY ALKYLTOLUENE. 